US20110182790A1 - Transition metal-containing aluminosilicate zeolite - Google Patents

Transition metal-containing aluminosilicate zeolite Download PDF

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Publication number
US20110182790A1
US20110182790A1 US13/057,911 US200913057911A US2011182790A1 US 20110182790 A1 US20110182790 A1 US 20110182790A1 US 200913057911 A US200913057911 A US 200913057911A US 2011182790 A1 US2011182790 A1 US 2011182790A1
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United States
Prior art keywords
aluminosilicate zeolite
zeolite catalyst
group
aluminosilicate
transition metal
Prior art date
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Abandoned
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US13/057,911
Inventor
Guy Richard Chandler
Neil Robert Collins
Rodney Foo Kok Shin
Alexander Nicholas Michael Green
Paul Richard Phillips
Raj Rao Rajaram
Stuart David Reid
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Johnson Matthey PLC
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Johnson Matthey PLC
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Application filed by Johnson Matthey PLC filed Critical Johnson Matthey PLC
Assigned to JOHNSON MATTHEY PUBLIC LIMITED COMPANY reassignment JOHNSON MATTHEY PUBLIC LIMITED COMPANY ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: CHANDLER, GUY RICHARD, GREEN, ALEXANDER NICHOLAS MICHAEL, REID, STUART DAVID, COLLINS, NEIL ROBERT, PHILLIPS, PAUL RICHARD, RAJARAM, RAJ RAO, SHIN, RODNEY FOO KOK
Publication of US20110182790A1 publication Critical patent/US20110182790A1/en
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    • B01D2255/207—Transition metals
    • B01D2255/20761—Copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/50—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • B01J35/60—
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2370/00—Selection of materials for exhaust purification
    • F01N2370/02—Selection of materials for exhaust purification used in catalytic reactors
    • F01N2370/04—Zeolitic material
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/12—Improving ICE efficiencies

Definitions

  • the present invention relates to a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal.
  • the zeolites can be used for selective catalytic reduction (SCR) of nitrogen oxides in exhaust gases, such as exhaust gases from internal combustion engines, using a nitrogenous reductant.
  • U.S. Pat. No. 4,544,538 discloses a synthetic zeolite having a crystal structure of chabazite (CHA), designated SSZ-13 prepared using a Structure Directing Agent (SDA) such as the N,N,N-trimethyl-1-adamantammonium cation.
  • SDA Structure Directing Agent
  • the SSZ-13 can be ion exchanged with transition metals such as rare earth, Mn, Ca, Mg, Zn, Cd, Pt, Pd, Ni, Co, Ti, Al, Sn, Fe and Co for use e.g. in hydrocarbon conversion reactions.
  • U.S. Pat. No. 6,709,644 discloses a synthetic zeolite having a crystal structure of chabazite (CHA) of small crystallite size (on average ⁇ 0.5 micrometers) designated SSZ-62.
  • SSZ-62 can also be prepared using the N,N,N-trimethyl-1-adamantammonium cation SDA.
  • Example 1 of U.S. Pat. No. 6,709,644 compares the average crystal size of SSZ-62 with the average crystal size of SSZ-13.
  • SSZ-62 can be used in a process for converting lower alcohols or the zeolite can be exchanged with copper or cobalt for use in catalysing the reduction of NO x in a lean gas stream e.g. of an internal combustion engine.
  • a lean gas stream e.g. of an internal combustion engine.
  • the activity of small and large crystallite size materials are only illustrated by a methanol to olefin reaction.
  • transition metal/zeolite catalysts such as Cu/Beta and/or Fe/Beta are being considered for urea and/or NH 3 SCR of NO x from mobile diesel engines to meet new emission standards.
  • These catalysts are required to withstand relatively high temperatures under exhaust conditions, and may also be exposed to relatively high levels of hydrocarbons (HC), which can be adsorbed onto or into the pores of the zeolites.
  • HC hydrocarbons
  • the adsorbed HC may affect the NH 3 SCR activities of these metal zeolites catalysts by blocking the active sites or blocking access to the active sites for the NH 3 —NO x reaction.
  • these adsorbed HC species may be oxidised as the temperature of the catalytic system is raised, generating a significant exotherm, which can thermally or hydrothermally damage the catalyst. It is therefore desirable to minimise HC adsorption on the SCR catalyst, especially during cold start when significant amounts of HC can be emitted from the engine.
  • the invention provides a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer.
  • the at least one catalytically active transition metal is one of copper and iron.
  • the zeolite can contain both copper and iron.
  • the Examples show a trend of increasing NO x reduction activity of fresh and aged copper/CHA catalysts with increasing crystallite size.
  • Scanning electron microscopy can determine the morphology and crystallite size of zeolites according to the invention. It is desirable that the mean particle size of the aluminosilicate zeolite as measured by SEM is >0.50 micrometer, but preferably greater than 1.00 micrometer, such as >1.50 micrometers. In embodiments, the mean crystallite size is ⁇ 15.0 micrometers, such as ⁇ 10.0 micrometers or ⁇ 5.0 micrometers.
  • the aluminosilicate zeolite catalyst according to the invention is selected from the group consisting of zeolites having a maximum ring size of eight tetrahedral atoms especially Framework Type Codes CHA, ERI and LEV, most preferably CHA.
  • an isotype framework structure of CHA can be selected from the group consisting of, for example, Linde-D, Linde-R, SSZ-13, LZ-218, Phi and ZK-14.
  • a type material or isotype framework structure of ERI Framework Type Code zeolites can be, for example, erionite, ZSM-34 or Linde Type T.
  • LEV Framework Type Code isotype framework structures or type material can be, for example, levynite, Nu-3, LZ-132 or ZK-20.
  • the total at least one transition metal present in the catalyst is from 0.1 to 10.0 wt % based on the total weight of the zeolite catalyst, such as 0.5 to 5.0 wt % based on the total weight of the zeolite catalyst.
  • the invention provides a method of converting nitrogen oxides in a gas to nitrogen by contacting the nitrogen oxides with a nitrogenous reducing agent in the presence of an aluminosilicate zeolite catalyst according to the invention.
  • the nitrogen oxides can be reduced with the reducing agent at a temperature of at least 100° C., for example from about 150° C. to 750° C.
  • the nitrogen oxides reduction is performed in the presence of oxygen.
  • nitrogenous reductant can be controlled so that NH 3 at the zeolite catalyst inlet is controlled to be 60% to 200% of theoretical ammonia calculated at 1:1 NH 3 /NO and 4:3 NH 3 /NO 2 .
  • nitrogen monoxide in the gas is oxidised to nitrogen dioxide using an oxidation catalyst located upstream of the zeolite catalyst and the resulting gas is then mixed with nitrogenous reductant before the mixture is fed into the zeolite catalyst, wherein the oxidation catalyst is adapted to yield a gas stream entering the zeolite catalyst having a ratio of NO to NO 2 of from about 4:1 to about 1:3 by volume.
  • the nitrogenous reductant can be ammonia per se, hydrazine or an ammonia precursor selected from the group consisting of urea ((NH 2 ) 2 C0), ammonium carbonate, ammonium carbamate, ammonium hydrogen carbonate and ammonium formate.
  • the gas containing nitrogen oxides to be treated with the method according to the present invention can be derived from a combustion process, particularly from an internal combustion engine such as a stationary source or preferably a vehicular lean burn internal combustion engine.
  • the invention provides an exhaust system for a vehicular lean-burn internal combustion engine, which system comprising a conduit for carrying a flowing exhaust gas, a source of nitrogenous reductant, a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, disposed in a flow path of the exhaust gas and means for metering nitrogenous reductant into a flowing exhaust gas upstream of the zeolite catalyst, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer.
  • Small crystallite CHA was prepared according to Example 1 of U.S. Pat. No. 6,709,644 (the entire contents of which is incorporated herein by reference).
  • a reaction mixture was prepared of molar composition 60 SiO 2 .1.5 Al 2 O 3 -6 Na 2 O-12 NNNAnOH-2640 H 2 O, where NNNAnOH is the structure directing agent (SDA) or template N,N,N-trimethyladamantanammonium hydroxide
  • the reaction was prepared using cab-o-sil M5 (Cabot Corporation) as the source of silica, sodium aluminate (BDH Ltd), sodium hydroxide (Alfa Aesar).
  • the SDA NNAnOH
  • the required amount of the SDA solution was weighed out and the NaOH added and stirred until it dissolved.
  • the sodium aluminate solid was then added with stirring and stirring was continued until it dissolved.
  • the cab-o-sil was then mixed in and the resulting mixture transferred to a 1 L stainless steel autoclave. The autoclave was sealed and the mixture heated to 165 C with stirring (300 rpm) for 4 days.
  • the resulting product was identified as a CHA type material by powder x-ray diffraction. Visually, the product crystals were approximately 2 microns on edge.
  • the product composition had a silica-alumina ratio (SAR) of 24:1.
  • Copper was deposited on zeolites A, B and C prepared according to Example 1 by the standard wet impregnation method using copper acetate as the copper precursor.
  • aluminosilicate zeolite 0.471 g of copper acetate was dissolved in a sufficient amount of water to wet the aluminosilicate zeolite material. The solution was added to the aluminosilicate zeolite material and stirred. The wet powder was dried at 105° C., before being calcined at 500° C. for 2 hours. Following calcination, a majority of the copper is understood to be present as copper (II) oxide.
  • Catalysts A, B and C The copper-loaded catalysts prepared according to this Example were designated as Catalysts A, B and C.
  • Catalysts prepared according to Example 2 are referred to as “Fresh Catalysts A-C”.
  • Fresh Catalysts A-C prepared according to Example 2 were hydrothermally aged in an atmosphere containing 10% oxygen, 10% water, balance nitrogen at 750° C. for a period of 24 hours.
  • the hydrothermally aged catalyst is referred to as “Aged Catalysts A-C”.
  • Counting and sizing was determined by number averaged digital particle size analysis, based on “thresholding” the intensities from each pixel of an image, and exploiting the differences in intensity between particles and the background. The software assumes that each object detected is circular/spherical.
  • the NO x conversion of Catalysts A-C of Examples 2 and 3 at an inlet gas temperature of 200° C. or 400° C. are given in Table 2.
  • the NO x reduction performance was measured on a powder sample in a laboratory reactor by ramping the catalyst at 5° C. per minute in a gas mixture containing 500 ppm NO and NH 3 , 10% O 2 , 10% H 2 O and N 2 .

Abstract

A synthetic alumino silicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which alumino silicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer.

Description

  • The present invention relates to a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal. The zeolites can be used for selective catalytic reduction (SCR) of nitrogen oxides in exhaust gases, such as exhaust gases from internal combustion engines, using a nitrogenous reductant.
  • It is known to convert oxides of nitrogen (NOx) in a gas to nitrogen by contacting the NOx with a nitrogenous reducing agent, e.g. ammonia or an ammonia precursor such as urea, in the presence of a zeolite catalyst containing at least one transition metal, and it has been suggested to adopt this technique for treating NOx emitted from vehicular lean-burn internal combustion engines, see for example DieselNet Technology Guide “Selective Catalytic Reduction” Revision 2005.05d, by W. Addy Majewski published on www.dieselnet.com.
  • U.S. Pat. No. 4,544,538 discloses a synthetic zeolite having a crystal structure of chabazite (CHA), designated SSZ-13 prepared using a Structure Directing Agent (SDA) such as the N,N,N-trimethyl-1-adamantammonium cation. The SSZ-13 can be ion exchanged with transition metals such as rare earth, Mn, Ca, Mg, Zn, Cd, Pt, Pd, Ni, Co, Ti, Al, Sn, Fe and Co for use e.g. in hydrocarbon conversion reactions.
  • U.S. Pat. No. 6,709,644 discloses a synthetic zeolite having a crystal structure of chabazite (CHA) of small crystallite size (on average <0.5 micrometers) designated SSZ-62. SSZ-62 can also be prepared using the N,N,N-trimethyl-1-adamantammonium cation SDA. Example 1 of U.S. Pat. No. 6,709,644 compares the average crystal size of SSZ-62 with the average crystal size of SSZ-13. The document suggests that SSZ-62 can be used in a process for converting lower alcohols or the zeolite can be exchanged with copper or cobalt for use in catalysing the reduction of NOx in a lean gas stream e.g. of an internal combustion engine. However, the activity of small and large crystallite size materials are only illustrated by a methanol to olefin reaction.
  • In our International patent application no. PCT/GB2008/001451 filed 24 Apr. 2008 we explain that transition metal/zeolite catalysts such as Cu/Beta and/or Fe/Beta are being considered for urea and/or NH3SCR of NOx from mobile diesel engines to meet new emission standards. These catalysts are required to withstand relatively high temperatures under exhaust conditions, and may also be exposed to relatively high levels of hydrocarbons (HC), which can be adsorbed onto or into the pores of the zeolites. The adsorbed HC may affect the NH3SCR activities of these metal zeolites catalysts by blocking the active sites or blocking access to the active sites for the NH3—NOx reaction. Furthermore, these adsorbed HC species may be oxidised as the temperature of the catalytic system is raised, generating a significant exotherm, which can thermally or hydrothermally damage the catalyst. It is therefore desirable to minimise HC adsorption on the SCR catalyst, especially during cold start when significant amounts of HC can be emitted from the engine.
  • In our PCT/GB2008/001451 we suggest that both of these disadvantages of larger pore zeolite catalysts can be reduced or overcome by using small pore zeolites, which generally allow the diffusion of NH3 and NOx to the active sites inside the zeolite pores, but which generally hinder diffusion of hydrocarbon molecules into the pores. Zeolites that have the small pore dimensions to induce this shape selectivity whereby larger hydrocarbons are prevented from accessing the active metal sites within the zeolite cavities include CHA, ERI and LEV. Additionally, small pore zeolite-based SCR catalysts produce less N2O as a by-product of the NOx reduction reaction.
  • We have researched into aluminosilicate zeolite materials and have discovered, very surprisingly, that large crystallite aluminosilicate zeolite materials have higher activity for the SCR process using a nitrogenous reductant than the same aluminosilicate zeolite material of smaller crystallite size.
  • According to one aspect, the invention provides a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer. Preferably, the at least one catalytically active transition metal is one of copper and iron. In embodiments, the zeolite can contain both copper and iron.
  • The Examples show a trend of increasing NOx reduction activity of fresh and aged copper/CHA catalysts with increasing crystallite size.
  • Scanning electron microscopy can determine the morphology and crystallite size of zeolites according to the invention. It is desirable that the mean particle size of the aluminosilicate zeolite as measured by SEM is >0.50 micrometer, but preferably greater than 1.00 micrometer, such as >1.50 micrometers. In embodiments, the mean crystallite size is <15.0 micrometers, such as <10.0 micrometers or <5.0 micrometers.
  • In embodiments, the aluminosilicate zeolite catalyst according to the invention is selected from the group consisting of zeolites having a maximum ring size of eight tetrahedral atoms especially Framework Type Codes CHA, ERI and LEV, most preferably CHA.
  • Where the Framework Type Code of the aluminosilicate zeolite is CHA, an isotype framework structure of CHA can be selected from the group consisting of, for example, Linde-D, Linde-R, SSZ-13, LZ-218, Phi and ZK-14.
  • A type material or isotype framework structure of ERI Framework Type Code zeolites can be, for example, erionite, ZSM-34 or Linde Type T.
  • LEV Framework Type Code isotype framework structures or type material can be, for example, levynite, Nu-3, LZ-132 or ZK-20.
  • The total at least one transition metal present in the catalyst is from 0.1 to 10.0 wt % based on the total weight of the zeolite catalyst, such as 0.5 to 5.0 wt % based on the total weight of the zeolite catalyst.
  • According to another aspect, the invention provides a method of converting nitrogen oxides in a gas to nitrogen by contacting the nitrogen oxides with a nitrogenous reducing agent in the presence of an aluminosilicate zeolite catalyst according to the invention.
  • The nitrogen oxides can be reduced with the reducing agent at a temperature of at least 100° C., for example from about 150° C. to 750° C.
  • In a particular embodiment, the nitrogen oxides reduction is performed in the presence of oxygen.
  • The addition of nitrogenous reductant can be controlled so that NH3 at the zeolite catalyst inlet is controlled to be 60% to 200% of theoretical ammonia calculated at 1:1 NH3/NO and 4:3 NH3/NO2.
  • In a particular embodiment, wherein nitrogen monoxide in the gas is oxidised to nitrogen dioxide using an oxidation catalyst located upstream of the zeolite catalyst and the resulting gas is then mixed with nitrogenous reductant before the mixture is fed into the zeolite catalyst, wherein the oxidation catalyst is adapted to yield a gas stream entering the zeolite catalyst having a ratio of NO to NO2 of from about 4:1 to about 1:3 by volume.
  • In the method according to the invention, the nitrogenous reductant can be ammonia per se, hydrazine or an ammonia precursor selected from the group consisting of urea ((NH2)2C0), ammonium carbonate, ammonium carbamate, ammonium hydrogen carbonate and ammonium formate.
  • The gas containing nitrogen oxides to be treated with the method according to the present invention can be derived from a combustion process, particularly from an internal combustion engine such as a stationary source or preferably a vehicular lean burn internal combustion engine.
  • According to another aspect, the invention provides an exhaust system for a vehicular lean-burn internal combustion engine, which system comprising a conduit for carrying a flowing exhaust gas, a source of nitrogenous reductant, a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, disposed in a flow path of the exhaust gas and means for metering nitrogenous reductant into a flowing exhaust gas upstream of the zeolite catalyst, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer.
  • In order that the invention may be more fully understood, the following Examples are provided by way of illustration only.
    • EXAMPLE 1 Preparation of Zeolite Samples Zeolite A
  • Small crystallite CHA was prepared according to Example 1 of U.S. Pat. No. 6,709,644 (the entire contents of which is incorporated herein by reference).
    • Zeolite B
  • Large crystallite CHA was prepared according to a method of making SSZ-13 by S. I. Zones and R A. Van Nordstrand, Zeolites 8 (1988) 166 (the entire contents of which is incorporated herein by reference) also published on International Zeolite Association Synthesis Commission website http://www.iza-online.org/synthesis/, as follows:
      • The source materials were:
      • sodium hydroxide (1 N), (Baker, reagent grade);
      • N,N,N, trimethyl-1-adamantanammonium hydroxide (RN—OH)(0.72M);
      • deionized water;
      • aluminium hydroxide (Reheis F-2000 dried gel, 50% Al2O3); and
      • fumed silica (Cab-Q-Sil, M5 grade, 97% SiO2).
      • The reaction mixture was prepared as follows:
      • (1) 2.00 g 1N NaOH+2.78 g 0.72 M RNOH+3.22 g water, add sequentially to a Teflon cup of a Parr 23 mL autoclave;
      • (2) (1)+0.05 g aluminum hydroxide, mix until solution clears;
      • (3) (2)+0.60 g fumed silica, mix until uniform.
      • The reaction mixture was crystallised:
      • in a teflon-lined 23 mL autoclave (Parr model 4745) at a temperature of 160° C. for 4 days without agitation;
      • After cooling to room temperature the mixture was filtered, washed with de-mineralised water and air-dried overnight.
      • The resulting product was characterised by powder x-ray diffraction and identified as:
      • CHA zeolite with a SiO2/Al2O3 ratio of 28 as determined by ICP.
      • SEM analysis showed:
      • cubes of 2-5 micrometers.
    Zeolite C
  • A reaction mixture was prepared of molar composition 60 SiO2.1.5 Al2O3-6 Na2O-12 NNNAnOH-2640 H2O, where NNNAnOH is the structure directing agent (SDA) or template N,N,N-trimethyladamantanammonium hydroxide
  • The reaction was prepared using cab-o-sil M5 (Cabot Corporation) as the source of silica, sodium aluminate (BDH Ltd), sodium hydroxide (Alfa Aesar). The SDA (NNNAnOH) was prepared following the method described in U.S. Pat. No. 4,544,538 (the entire contents of which is incorporated herein by reference). The required amount of the SDA solution was weighed out and the NaOH added and stirred until it dissolved. The sodium aluminate solid was then added with stirring and stirring was continued until it dissolved. The cab-o-sil was then mixed in and the resulting mixture transferred to a 1 L stainless steel autoclave. The autoclave was sealed and the mixture heated to 165 C with stirring (300 rpm) for 4 days.
  • The resulting product was identified as a CHA type material by powder x-ray diffraction. Visually, the product crystals were approximately 2 microns on edge. The product composition had a silica-alumina ratio (SAR) of 24:1.
    • EXAMPLE 2 Preparation of 3 wt % Cu/aluminosilicate zeolite
  • Copper was deposited on zeolites A, B and C prepared according to Example 1 by the standard wet impregnation method using copper acetate as the copper precursor. For 10 g of aluminosilicate zeolite, 0.471 g of copper acetate was dissolved in a sufficient amount of water to wet the aluminosilicate zeolite material. The solution was added to the aluminosilicate zeolite material and stirred. The wet powder was dried at 105° C., before being calcined at 500° C. for 2 hours. Following calcination, a majority of the copper is understood to be present as copper (II) oxide.
  • The copper-loaded catalysts prepared according to this Example were designated as Catalysts A, B and C. Catalysts prepared according to Example 2 are referred to as “Fresh Catalysts A-C”.
    • EXAMPLE 3 Hydrothermal Ageing
  • Fresh Catalysts A-C prepared according to Example 2 were hydrothermally aged in an atmosphere containing 10% oxygen, 10% water, balance nitrogen at 750° C. for a period of 24 hours. The hydrothermally aged catalyst is referred to as “Aged Catalysts A-C”.
  • TABLE 1
    surface area, silica alumina ratio, crystal size and
    copper loading of the different catalysts (fresh).
    Chabazite Silica to Average SEM
    Alumino- alumina Crystal
    silicate BET surface ratio Dimension Cu loading
    code area (SAR) (micrometer)* wt %
    A 784 26 0.15 3
    B 634 24 0.5 3
    C 616 24 1.4 3
    *The samples were dispersed in methanol and subjected to ultrasound for 20 mins and a drop of this liquid was put on a standard carbon padded Scanning Electron Microscope (SEM) stub.

    Counting and sizing was determined by number averaged digital particle size analysis, based on “thresholding” the intensities from each pixel of an image, and exploiting the differences in intensity between particles and the background. The software assumes that each object detected is circular/spherical.
    • EXAMPLE 4 Activity Tests
  • The NOx conversion of Catalysts A-C of Examples 2 and 3 at an inlet gas temperature of 200° C. or 400° C. are given in Table 2. The NOx reduction performance was measured on a powder sample in a laboratory reactor by ramping the catalyst at 5° C. per minute in a gas mixture containing 500 ppm NO and NH3, 10% O2, 10% H2O and N2.
  • TABLE 2
    NOx conversion at a catalyst inlet gas temperature of 200° C. and
    400° C. for Fresh and 750° C. 24 hour-Aged Conditions
    Average
    SEM Crystal Cu 500° C. Calcined 750° C. Aged
    Dimension Loading % NOx Conversion % NOx Conversion
    Catalyst SAR (micrometer) † wt % 190° C. 200° C. 400° C. 190° C. 200° C. 400° C.
    A 26 0.15 3 73 86 99 44 58 96
    B 24 0.5 3 85 95 99 51 66 97
    C 24 1.4 3 87 97 99 68 83 99
    † See notes on Table 1.
  • It can be seen from Table 2 that the activity of the catalysts generally follows a trend of increasing activity with crystallite size. Hence we conclude that larger crystallite size aluminosilicate zeolite materials are surprisingly more active either fresh or hydrothermally aged than catalysts prepared from smaller crystals of the same aluminosilicate zeolite material.

Claims (23)

1. A synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer.
2. An aluminosilicate zeolite catalyst according to claim 1, wherein the at least one catalytically active transition metal is copper, iron or copper and iron.
3. (canceled)
4. An aluminosilicate zeolite catalyst according to claim 1, wherein the mean crystallite size is >1.00 micrometer
5. An aluminosilicate zeolite catalyst according to claim 1, wherein the mean crystallite size is >1.50 micrometers.
6. An aluminosilicate zeolite catalyst according to claim 1, wherein the mean crystallite size is <15.00 micrometers.
7. An aluminosilicate zeolite catalyst according to claim 1, wherein the aluminosilicate zeolite is selected from the group consisting of Framework Type Codes CHA, ERI and LEV.
8. (canceled)
9. An aluminosilicate zeolite catalyst according to claim 1, wherein the aluminosilicate zeolite has Framework Type Code CHA and isotype framework structures of CHA are selected from the group consisting of Linde-D, Linde-R, SSZ-13, LZ-218, Phi and ZK-14.
10. An aluminosilicate zeolite catalyst according to claim 1, wherein the aluminosilicate zeolite has Framework Type Code ERI and a type material or isotype framework structures of ERI are erionite, ZSM-34 or Linde Type T.
11. An aluminosilicate zeolite catalyst according to claim 1, wherein the aluminosilicate zeolite has Framework Type Code LEV and a type material or isotype framework structures of LEV are levynite, Nu-3, LZ-132 or ZK-20.
12. An aluminosilicate zeolite catalyst according to claim 1, wherein the total at least one transition metal present in the catalyst is from 0.1 to 10.0 wt % based on the total weight of the zeolite catalyst.
13. (canceled)
14. A method of converting nitrogen oxides in a gas to nitrogen by contacting the nitrogen oxides with a nitrogenous reducing agent in the presence of a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer.
15. A method according to claim 14, wherein the nitrogen oxides are reduced with the reducing agent at a temperature of at least 100° C.
16. A method according to claim 15, wherein the temperature is from about 150° C. to 750° C.
17. A method according to claim 14, wherein the nitrogen oxides reduction is performed in the presence of oxygen.
18. A method according to claim 14, wherein addition of nitrogenous reductant is controlled so that NH3 at the zeolite catalyst inlet is controlled to be 60% to 200% of theoretical ammonia calculated at 1:1 NH3/NO and 4:3 NH3/NO2.
19. A method according to claim 14, wherein nitrogen monoxide in the gas is oxidised to nitrogen dioxide using an oxidation catalyst located upstream of the zeolite catalyst and the resulting gas is then mixed with nitrogenous reductant before the mixture is fed into the zeolite catalyst, wherein the oxidation catalyst is adapted to yield a gas stream entering the zeolite catalyst having a ratio of NO to NO2 of from about 4:1 to about 1:3 by volume.
20. A method according to claim 14, wherein the nitrogenous reductant is ammonia per se, hydrazine or an ammonia precursor selected from the group consisting of urea ((NH2)2CO), ammonium carbonate, ammonium carbamate, ammonium hydrogen carbonate and ammonium formate.
21. A method according to claim 14, wherein the gas containing nitrogen oxides is derived from a combustion process.
22. A method according to claim 21, wherein the combustion process is the combustion of fuel in a vehicular lean burn internal combustion engine.
23. An exhaust system for a vehicular lean-burn internal combustion engine, which system comprising a conduit for carrying a flowing exhaust gas, a source of nitrogenous reductant, a synthetic aluminosilicate zeolite catalyst containing at least one catalytically active transition metal selected from the group consisting of Cu, Fe, Hf, La, Au, In, V, lanthanides and Group VIII transition metals, which aluminosilicate zeolite is a small pore aluminosilicate zeolite having a maximum ring size of eight tetrahedral atoms, disposed in a flow path of the exhaust gas and means for metering nitrogenous reductant into a flowing exhaust gas upstream of the zeolite catalyst, wherein the mean crystallite size of the aluminosilicate zeolite determined by scanning electron microscope is >0.50 micrometer.
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Owner name: JOHNSON MATTHEY PUBLIC LIMITED COMPANY, UNITED KIN

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